Method and apparatus for removing solute from a solid solute-bearing product

ABSTRACT

The process and apparatus are for removing a solute from a solute-bearing solid product by means of a solvent which remains in liquid state throughout the entire oil extraction process. In one embodiment, the solvent is normally in gazeous state at ambient temperature and pressure values, but is used mainly in liquid state within the method and apparatus of the present invention by maintaining such pressure and temperature values within the apparatus so that the solvent will remain in this liquid state.

CROSS-REFERENCE DATA

The present application is a Continuation application of co-pendingpatent application Ser. No. 11/011,639 filed on Dec. 14, 2004, which isa Continuation-in-Part of application Ser. No. 10/892,064, filed on Jul.14, 2004, now abandoned, which claims the benefit of application No.60/486,743, filed on Jul. 14, 2003, which is incorporated herein byreference.

FIELD OF THE INVENTION

The present invention generally relates to a method and apparatus forremoving solute from solute-bearing solid product, and more particularlyto a method and apparatus for removing oil from an oil-bearing solidproduct by means of a solvent that leaches the oil from the oil-bearingproduct.

BACKGROUND OF THE INVENTION

Processes for removing oil from solid oil-bearing products are known inthe art. Some such processes occur in an extraction chamber where asolvent is sprayed or otherwise injected on the oil-bearing product, toleach the oil out of the solid product. There results a miscellacomprising a mixture of oil and solvent, which is conveyed to anoil-solvent separation chamber.

Some processes make use of a liquid solvent which is liquid at givenextraction temperature and pressure values, but which is normallygazeous at ambient temperature and pressure values. After having leachedthe oil out of the solid product with the liquid-state solvent in theextraction chamber, the miscella is separated into its distinct oil andsolvent components in the separation chamber which is heated to such atemperature that the solvent becomes gazeous while the oil remainsliquid, thus allowing the oil and solvent to be easily distinctlycollected.

One problem associated to such prior art processes is that the oil andthe solids will often be denatured by the application of heat to thesolids and/or oil, which is undesirable. Denaturing is defined as anyphysical, chemical or molecular change in the solute or solid product.This is especially true, in prior art processes, during the separationphase of the miscella, where relatively high oil-denaturing temperaturesare often reached.

SUMMARY OF THE INVENTION

The present invention relates to a process for separating a solute froma solute-bearing solid product comprising the steps of:

providing an extraction chamber with determined extraction pressure andtemperature values;

controlling said extraction pressure to maintain it above an ambientpressure value;

controlling said extraction temperature to maintain it at a temperaturethat will not denature said solute nor said solid product;

feeding said solute-bearing solid product in said extraction chamber;

providing a solvent which is in mainly liquid state at said extractionpressure and temperature values, with said solute being soluble in saidsolvent at said extraction pressure and temperature values;

injecting said solvent in liquid state on said solute-bearing product insaid extraction chamber for leaching said solute from said solid productwith said solvent;

distinctly recuperating said solid product from which at least a portionof said solute has been leached, and a miscella comprising a mixture ofsaid solvent and said solute leached from said solid product;

conveying said miscella to a separation unit with determined separationtemperature and pressure values, with said solvent remaining mainly inliquid state at said separation temperature and pressure values, andwith said separation unit temperature value being controlled to maintainit at a temperature that will not denature said solute;

separating said solvent from said solute in said separation unit througha liquid-liquid separation process; and

distinctly recuperating said solvent and said solute separated in saidseparation unit; wherein said solvent remains mainly in a liquid-statethroughout said process.

In one embodiment, said solvent is in gazeous state at ambienttemperature and pressure values but mainly in liquid-state at saidextraction temperature and pressure values.

In one embodiment, said extraction and separation temperatures are equalto ambient temperature, with said solvent being maintained mainly inliquid-state throughout said process by means of said extraction andseparation pressures being maintained above ambient pressure.

In one embodiment, said solvent recuperated from said separation unit isreutilized within said extraction chamber for extracting additionalsolute from additional said solute-beating material, whereby saidsolvent is used within a closed-loop circuit and remains mainly inliquid state throughout said closed-loop circuit.

In one embodiment, said liquid-liquid separation process is one ofmolecular weight, specific gravity and viscosity differential separationprocesses.

In one embodiment, said process is a batch process, with the step offeeding said solute-bearing solid product in said extraction chamberbeing accomplished by loading a batch of solute-bearing solid product insaid extraction chamber.

In an alternate embodiment, said process is a continuous process, withthe step of feeding said solute-bearing solid product in said extractionchamber being accomplished by continuously circulating thesolute-bearing product through said extraction chamber and continuouslyrecuperating solid product from which at least a portion of oil has beenleached at an outlet of said extraction chamber.

In one embodiment, said extraction chamber comprises a number ofextraction chamber portions through which said solute-bearing product issequentially circulated for extracting solute from the solute-bearingsolid product, with each extraction chamber portion definingcorresponding extraction chamber parameters and with at least someextraction chamber parameters differing from one extraction chamber tothe other.

In one embodiment, the step of injecting said solvent in said extractionchamber is accomplished by means of at least one spray nozzle extendingin said extraction chamber capable of forming a vortex-shaped solventspray pattern.

In one embodiment, the step of continuously circulating saidsolute-bearing product through said extraction chamber is accomplishedby means of an auger equipped with agitation paddles, said processfurther comprising the step of agitating particles of saidsolute-bearing product to promote the formation of free-floating solidproduct particles that will be at least partly carried into saidvortex-shaped solvent spray pattern.

In one embodiment, the step of controlling said extraction pressure tomaintain it above an ambient pressure value is accomplished by means ofa gas injector injecting in said extraction chamber one of a vapor ofsaid solvent and a gas which is unreactive with said solvent, oil andsolid product.

The present invention also relates to an apparatus for separating oilfrom an oil-bearing solid product comprising:

an extraction chamber;

a solvent injector for injecting solvent in said extraction chamber forleaching oil from the oil-bearing solid product to form a miscellacomprising a mixture of solvent and oil;

a miscella outlet in said extraction chamber for collecting miscella;and

a liquid-liquid separation unit linked to said miscella outlet, forseparating the miscella into its respective oil and solvent components;

wherein solvent injected in said extraction chamber remains mainly inliquid state to leach oil from the oil-bearing product to form therewiththe miscella, and remains mainly in liquid state in said liquid-liquidseparation unit.

In one embodiment, the apparatus further comprises:

an inlet valve located upstream of said extraction chamber and allowingsaid oil-bearing solid product to enter said extraction chamber withoutallowing the passage of fluid between said extraction chamber and theatmosphere;

an outlet valve located downstream of said extraction chamber andallowing the solid product from which oil has been leached to exit saidextraction chamber without allowing the passage of fluid between saidextraction chamber and the atmosphere; and

an impeller for circulating said solid product from said inlet valvethrough said extraction chamber towards said outlet valve;

wherein said apparatus allows the continuous feeding of solid product tosaid inlet valve, the continuous leaching of oil from the solid product,the continuous output of solid product from said outlet valve, and thecontinuous collection of miscella at said miscella outlet.

In one embodiment, the apparatus further comprises a security solventextraction unit downstream of said outlet valve, for removing residualsolvent vapors by the application of heat to the solid product.

The present invention further relates to a valve defining an inlet andan outlet, for allowing a solid product to pass from said inlet to saidoutlet while preventing fluids from being exchanged between said inletand outlet, comprising:

an inner channel extending between said inlet and said outlet;

a fluid exhaust port in said inner channel intermediate said inlet andoutlet, said fluid exhaust port being in communication with a vacuumpump and being equipped with a filter allowing passage of fluids throughsaid fluid exhaust port but preventing passage of the solid productthrough said fluid exhaust port;

a rotary valve member located in said inner channel and being rotatabletherein, said rotary valve member comprising a main body engaging saidinner channel in a fluid-tight manner and having an elongatedtransversal channel, said rotary valve member being capable of rotatingbetween a first position in which said transversal channel iscoextensive and communicates with said valve inner channel and in whichsaid main body obstructs said fluid exhaust port, and a second positionin which said transversal channel is in facing register and communicateswith said fluid exhaust port and said main body obstructs said valveinner channel; and

a piston longitudinally movable within said elongated transversalchannel between two limit positions.

DESCRIPTION OF THE DRAWINGS

In the annexed drawings:

FIG. 1 is a schematic view of an apparatus for carrying out the presentinvention according to a continuous process for removing oil from anoil-bearing product;

FIG. 2 is an enlarged schematic cross-sectional view of the inlet valveof the apparatus of FIG. 1;

FIGS. 3 to 5 are schematic cross-sectional views of the rotary valvemember only of the valve of FIG. 2, at a smaller scale, sequentiallyshowing the rotary valve member in three positions thereof andsuggesting the rotation of the valve member and the linear displacementof the piston with arrows;

FIG. 6 is a schematic cross-sectional view of an alternate embodiment ofa valve assembly according to the present invention that includes twovalves similar to the valve of FIG. 2;

FIG. 7 is a schematic longitudinal cross-sectional view of an extractionchamber according to the present invention;

FIG. 8 is a schematic cross-sectional view taken along line VIII-VIII ofFIG. 7; and

FIG. 9 is a schematic view of an alternate apparatus for carrying outthe present invention according to a batch process for removing oil froman oil-bearing product.

DETAILED DESCRIPTION OF THE EMBODIMENTS

The present invention generally relates to a method and apparatus forremoving a solute from a solute-bearing solid product by means of asolvent which remains in liquid state throughout the entire oilextraction process. In one embodiment, the solvent is normally ingazeous state at ambient temperature and pressure values, but is used inliquid state within the method and apparatus of the present invention bymaintaining such pressure and temperature values within the apparatus sothat the solvent will remain in this liquid state. In anotherembodiment, the solvent is already in liquid state at ambienttemperature and pressure values, and is maintained in this liquid statewithin the apparatus of the invention.

According to one embodiment of the invention, the solute-bearing productis a solid product containing a certain quantity of oil or fat. Thesolid product can be, for example, rendered animal tissue, industrial,commercial or domestic oleiferous wastes, oleiferous hazards, oleiferousindustrial byproducts, oil bearing sands, strata, mineral, rockformation, fried or soaked substances inedible and edible, legumes andtheir hulls and casings, seeds and their hulls and casings and/orshells, nuts and their hulls, casings and/or shells, tree leafs andbranches and roots, plant leafs and stems, basal leafs and branches androots, marine life whether organic, mammal or aquatic, field crops andvegetables of every kind, for the separation of the solids from the fatsand natural oils organically, intrinsically contained, held or suspendedby or in them.

The solvent can be any suitable solvent in which said solute will besoluble at determined extraction pressure and temperature values. In oneembodiment, as indicated hereinabove, the solvent will be in a gazeousstate at ambient temperature and pressure values, but will be maintainedin a liquid state at extraction pressure and temperature values. Thesolvent may be for example propane or butane mixtures, or a refrigerant.

It is understood that the method and apparatus of the present inventionmay be used with many different solvents, the exact nature of thesolvent depending mostly on the oil-bearing product and the oilcontained in the oil-bearing product.

More particularly, the process of the present invention for separating asolute from a solute-bearing solid product comprises the steps of:

providing an extraction chamber with determined extraction pressure andtemperature values;

controlling the extraction pressure to maintain it above an ambientpressure value;

controlling the extraction temperature to maintain it at a temperaturethat will not denature the solute nor the solid product;

feeding the solute-bearing solid product in the extraction chamber;

providing a solvent which is mainly in liquid state at the extractionpressure and temperature values, with the solute being soluble in thesolvent at the extraction pressure and temperature values;

injecting the solvent on the solute-bearing in the extraction chamberfor leaching the solute from the solid product with the solvent;

distinctly recuperating the solid product from which at least a portionof the solute has been leached, and a miscella comprising a mixture ofthe solvent and the solute leached from the solid product;

conveying the miscella to a separation unit with determined separationtemperature and pressure values, with the solvent remaining mainly inliquid state at the separation temperature and pressure values, and withthe separation unit temperature value being controlled to maintain it ata temperature that will not denature the solute;

separating the solvent from the solute in the separation unit throughone of molecular weight, specific gravity and viscosity differentialseparation processes; and

distinctly recuperating the solvent and the solute separated in theseparation unit; wherein the solvent remains in a liquid-statethroughout said process.

The process of the invention may be accomplished as a continuous or abatch process.

FIG. 1 is a schematic view of one embodiment of an apparatus 20 used tocarry out the process of the present invention as a continuous process.

Apparatus 20 comprises a feedstock inlet valve 22 connected to a numberof consecutively contiguous extraction chambers 24 a, 24 b, 24 c, 24 d,24 e, generally referred to as extraction chambers 24, that are in factextraction chamber portions part of a single extraction chamber, asfurther detailed hereinafter, since they are in fluid communication withone another. However, in an alternate embodiment which is notillustrated, extraction chamber 24 could be fluidly isolated by suitablevalves.

Downstream of extractions chambers 24 is a solid product outlet valve 26connected to an optional security solvent extraction unit 28.Oil-bearing product, or feedstock, which is to be treated by apparatus20 to distinctly recuperate the oil and the solid product therefrom, isconsequently fed through the feedstock inlet valve 22 and sequentiallycirculated through the consecutively contiguous extractions chambers 24where a determined proportion of oil will be extracted from the solidoil-bearing product, as detailed hereinafter. The solid product fromwhich the oil has been extracted is then conveyed through solid productoutlet valve 26, towards the outlet of apparatus 20 downstream ofsecurity solvent extraction unit 28.

Inlet and outlet valves 22, 26 are valves that allow a continuous orsubstantially continuous through-flow of solid product, while preventingthe through-flow of other fluids. Thus, the solid product may freelyflow through valves 22, 26, while there will be no fluid exchangebetween extraction chambers 24 and the atmosphere.

In one embodiment, to facilitate the treatment of the solid oil-bearingproduct, the solid product is fed through inlet valve 22 in a granularor pellet format, with the maximum particle size of the solid productbeing empirically selected and/or calculated for an optimized oil yield.

Determined extraction pressure and temperature values are set andmaintained within extraction chambers 24. More particularly, theextraction pressure is controlled to maintain it above ambient pressurevalue, and the extraction temperature is controlled to maintain it at atemperature that will not denature the oil or the solid oil-bearingproduct. These extraction temperature and pressure values are set toallow the solvent to be maintained in a liquid state within extractionchambers 24, while in one embodiment, this same solvent would be in agazeous state at ambient temperature and pressure values. For example,the extraction temperature can be substantially equal to ambienttemperature, for example between 1° C. (33° F.) and 40° C. (104° F.),and the extraction pressure can be maintained well above the ambientpressure value, for example at approximately 10 bars. However, theseexemplary extraction temperature and pressure values are not to beconsidered restrictive, as they may vary depending on the nature of theoil, the oil-bearing product and the solvent being used. Still,maintaining an ambient temperature value within extraction chambers 24has the advantage of helping to prevent most oils and solid productsform being denatured, since they would naturally be found at ambienttemperature anyway.

One way to maintain the extraction pressure above the ambient pressure,is to have a gas injector pump 29 a connected to a gas injector 29 whichinjects gas into extraction chambers 24. FIG. 1 shows a single gasinjector 29 for all extraction chambers 24, but it is understood thatmultiple gas injectors could be provided. The nature of the gas beinginjected will be discussed hereinafter.

A closed loop liquid solvent circuit is provided within apparatus 20, inwhich liquid-state solvent is circulated for use in extracting the oilfrom the oil-bearing product fed into extraction chambers 24. Moreparticularly, a main solvent tank 30 is provided in apparatus 20, withinwhich solvent is stored at such temperature and pressure values so as toremain mainly in liquid state. A solvent pump 32 conveys solvent frommain solvent tank 30 to a solvent manifold 34, the latter connected tosolvent injectors in the form of a number of independently controlledspray nozzles 36 a, 36 b, 36 c, 36 d, 36 e—generally referred to asspray nozzles 36—that will inject solvent in corresponding extractionchambers 24.

Since the solute is soluble in the solvent at the extraction pressureand temperature values, as the solvent is sprayed into extractionchambers 24, it leaches oil from the solid oil-bearing product, with thesolvent and oil forming a miscella that is recuperated, for examplethrough a filter (not shown in FIG. 1) that will prevent the solidproduct particles from flowing therethrough, while allowing the miscellato flow therethrough. The miscella is collected through correspondingmiscella outlet channels 38 a, 38 b, 38 c, 38 d, 38 e—generally referredto as miscella outlet channels 38. Miscella pumps 40 a, 40 b, 40 c, 40d, 40 e—generally referred to as miscella pumps 40, are connected tomiscella channels 38 to ensure an outflow of the miscella fromextraction chambers 24. Miscella thus recuperated is conveyed to amiscella collection tank 42. Although a single miscella tank has beenshown, it is understood that distinct miscella tanks corresponding toeach extraction chamber could also be used. A pump 44 conveys themiscella from miscella tank 42 through a particulate filter 46 and intoa separation unit 48 where the oil is separated from the liquid-statesolvent through a known liquid-liquid separation process, for exampleone of molecular weight, specific gravity and viscosity differentialseparation processes. Also, determined separation temperature andpressure values are maintained within separation unit 48, with thesolvent remaining mainly in liquid state at the separation temperatureand pressure values, and with the separation unit temperature valuebeing controlled to maintain it at a temperature that will not denaturethe oil. In one embodiment, the separation temperature and pressurevalues are identical to the extraction temperature and pressure values,for example approximately ambient temperature and 10 bars, respectively.

The solvent separated from the oil in separator unit 48 is then conveyedby means of a pump 50 back into main solvent tank 30, while the oilseparated from the solvent is collected at an oil outlet, after havingpassed through an optional segregation unit 52 that will remove anyremaining residual solvent vapors, if any.

Throughout the closed-loop solvent circuit, the solvent remains mainlyin liquid state at all times. In the present specification and claims,although it is indicated that the solvent remains in liquid state, it isunderstood that some liquid-state solvent will in fact evaporate unlessthe corresponding surrounding area within apparatus 20 is saturated withsolvent vapor—thus in any case some solvent vapor will in fact bepresent. The solvent will not be entirely in liquid state at all timeswithin apparatus 20. Consequently, when it is stated that the solventremains in liquid-state, it refers to the active solvent that will beinjected through injectors 36, leach the oil from the solid product,form a miscella with the oil, be carried to be separated in liquid statein separation unit 48, and then re-used to be injected through injectors36. Thus, apart from a proportion of solvent that will naturallyevaporate in non-saturated areas of apparatus 20, it can be said thatthe solvent will remain “mainly” in liquid state.

Maintaining the closed-loop solvent circuit in liquid state may beaccomplished for example by maintaining the temperature constant atapproximately an ambient temperature value and by maintaining anabove-ambient pressure value within the closed-loop solvent circuit.This is particularly advantageous since it will help prevent the oil andthe solid product circulated within apparatus 20 from being denaturedsince they will not be subjected to a considerable amount of heat whichis frequent in prior art devices.

In a normal operation mode of apparatus 20, most if not all theliquid-state solvent will be recuperated through the miscella withinextraction chambers 24. However, there may be some cases where thesolvent is not entirely removed from the solid product when it exitsextraction chambers 24, especially some solvent vapors which areresident in the extraction chambers 24 and that remain trapped in thesolid product. Thus, optional security solvent extraction unit 28 whichis located downstream of outlet valve 26 is used to remove the residualsolvent in the solid product by the application of heat to preventsolvent from accidentally exiting apparatus 20. This heat level isrelatively low, in that the temperature in the optional security solventextraction unit 28 will be well below a temperature that could denaturethe solid product processed therein.

If solvent is removed from the solid product in security solventextraction unit 28, it may be recuperated, liquefied and conveyed tomain solvent tank 30 by means of suitable pipes (not shown). The same istrue about solvent vapors recuperated in segregation unit 52. In caseswhere there is a net loss of least part of the solvent during the oilextraction process of the present invention, then an auxiliary solventtank 55 equipped with its pump 55 a can be included in apparatus 20 toprovide the required additional solvent to be distributed by manifold34.

Alternatively, solvent vapor recuperated in security solvent extractionunit 28 can be conveyed to gas injector 29 to be re-used for maintainingthe above-ambient pressure within extraction chambers 24. Indeed, it ispossible to have solvent vapor-filled extraction chambers 24 whichallows the desired pressure to be maintained therein. This does notchange the fact that the solvent injected in liquid-state in extractionchambers 24 to leach the oil out of the solid product, will remainmainly in liquid state throughout the process of the present invention.Indeed, the solvent vapor is used to maintain the required pressure, andalthough a natural exchange between the gazeous-state solvent and theliquid-state solvent will occur, the liquid-state solvent mainly remainsin its liquid state. Alternately, if solvent vapor is not used to setand maintain the above-ambient pressure in extraction chambers 24, thenanother gas can be used in gas injector 29 that will not react with theoil, the solvent or the solid product, for example an inert gas oranother unreactive gas such as nitrogen.

An optional heating device 53 is provided between extraction chambers 24and outlet valve 26. Heating device 53 is equipped with heating means,for example in the form of a heating element 53 a, for slightly heatingthe solid product before it is submitted to a sensor device 51 thatdetects the oil content in the outputted solid product. This detectionof oil content may help the operator to properly set the extractionchamber parameters for obtaining a desired oil content in the solidproduct at the outlet of apparatus 20. Known sensors such as sensor 51work optimally at a constant temperature, and the purpose of heatingelement 53 is consequently to maintain the solid product at thisconstant temperature.

In one embodiment, shown in FIG. 1, inlet and outlet valves 22, 26 areeach connected to a vacuum pump 54 and to a compressor 56 that provideappropriate pressure differentials required to (a) prevent gases andfluids from the atmosphere outside of apparatus 20 (e.g. air) fromseeping within extraction chambers 24, and (b) prevent gases and fluidsfrom inside apparatus 20 (e.g. solvent vapors) from seeping outside ofapparatus 20 through valves 22, 26. Valves 22, 26 more particularlyinclude an intermediate chamber in which a vacuum will be created toremove all fluids therein such as air, before allowing the solidproducts to be conveyed downstream. Since there is a positive pressurewithin extraction chambers 24, compressor 56 will further act to pumpgas back into valves 22, 26. Some particular embodiments of valves 22,26 will now be discussed, although it is understood that the presentinvention is not limited thereto.

FIG. 2 shows a first embodiment of an inlet valve 22. Although valve 26will not be described in detail, it is understood that valve 26 would besimilar to valve 22. In the embodiment of FIG. 2, inlet valve 22comprises a hollow housing 200 comprising an inner channel 202 defininga feedstock inlet opening 204 opened to the ambient environment, afeedstock outlet opening 206 leading to extraction chambers 24 and afeedstock flow axis extending between inlet and outlet openings 204,206. An auger 208 is provided at inlet opening 204. Inlet opening may belocated at the bottom end of a hopper at least partly filled withfeedstock.

Housing 200 also comprises a widened intermediate portion 210 defining acylindrical inner channel portion 212 in which a complementarycylindrical rotary valve member 214 is rotatable about a rotation axiswhich is perpendicular to the feedstock flow axis. Rotary valve member214 defines a main body 215 that engages the valve inner channel 202 ina fluid-tight manner. Rotary valve member 214 comprises a transversalchannel 216 in which a piston 218 is longitudinally movable betweenfirst and second limit positions corresponding to the two extremities ofthe rotary valve member transversal channel 216.

An air exhaust port 220, equipped with a solid material filter 222 thatallows fluids to pass while preventing solids to pass, is provided onone side of the housing intermediate portion 210, being angularly spacedfrom the valve inner channel 202 at a 90° angle to the right-hand sideof FIG. 2. Air exhaust port 220 is connected to a selectively activatedvacuum pump (number 54 in FIG. 1) through a vacuum channel 224, and agas channel 226 in turn connected to a gas source (number 56 in FIG. 1)is also in communication with air exhaust port 220. The gas circulatingthrough gas channel 226 may be solvent vapor, or any other suitable gas,such as nitrogen for example, which would not chemically react with thesolvent, the oil or the solid product.

A solvent exhaust port 228 equipped with a solid material filter 230that allows fluids to pass while preventing solids to pass, is providedon the side of housing intermediate portion 210 opposite air exhaustport relative to valve inner channel 202—namely the left-hand side inFIG. 2. Solvent exhaust port 228 is thus angularly spaced from the valveinner channel 202 of a 90° angle and from the air exhaust port of a 180°angle. Solvent exhaust port 228 is connected to a selectively activatedvacuum pump (number 54 in FIG. 1) through a vacuum channel 232, and toan air channel 234 which is connected to the outside atmosphere.

In use, valve 22 is initially in a position as shown in FIG. 2, withrotary valve member 214 positioned so that transversal channel 216 iscoextensive with valve inner channel 202, and with piston 218 beinglocated in a first limit position at or near the extremity oftransversal channel 216 which is closest to feedstock inlet opening 204.In this position of rotary valve 214, piston 218 is continuously biasedtowards its first limit position due to the above-ambient pressurewithin extraction chambers 24.

Feedstock, for example in the form of granular solid oil-bearingmaterial, can then be forced by auger 208 and by the force of gravity,down into the feedstock inlet opening 204 of valve 22. As feedstock isgradually fed therein, piston 218 will gradually be forced towards itssecond limit position, against the bias of the pressure withinextraction chambers 24. Eventually, piston 218 will reach its secondlimit position as shown in FIG. 3.

At this point, rotary valve member 214 is rotated of 90° clockwise asshown in FIG. 4, until the open end of transversal channel 216, i.e. theend of transversal channel 216 that is not obstructed by piston 218,comes in facing register with air exhaust port 220. A vacuum is thencreated in exhaust port 220 and consequently in transversal channel 216,to purge fluids from transversal chamber 216 by sucking all fluids outof transversal channel 216 through vacuum channel 224. Solids areretained in transversal channel 216 by filter 222. This consequentlyremoves all air from within the feedstock-filled transversal channel 216to prevent any air from being subsequently allowed into extractionchambers 24. Once the vacuum is obtained, the vacuum pump is stopped andgas such as solvent vapor is injected into transversal chamber throughgas channel 226, until the pressure within transversal channel 216becomes substantially equal to that within extraction chambers 24.

Once this is accomplished, rotary valve member 214 is rotated a secondtime in the same clockwise direction of 90° as shown in FIG. 5, untilthe open end of transversal channel 216 comes in facing register withthe feedstock outlet opening 206 of valve 22. Under the force ofgravity, and under piston 218 being pushed downward as new feedstock isfed through feedstock inlet opening 204 by auger 208, the feedstockpresent in transversal channel 216 will be forced out and throughfeedstock outlet opening 206.

It is noted that when rotary valve member 214 moves into a position inwhich its open end comes in facing register with the air exhaust port asshown in FIG. 4, its closed end, i.e. its end which is obstructed bypiston 218, then simultaneously comes in facing register with solventexhaust port 228. A vacuum is then created through vacuum channel 232 topurge all solvent which may be present in the small area at the veryextremity of transversal channel provided that piston 218 might not belocated exactly at its second limit position and that such a small areamay consequently exist. Gas exhaust port 228 thus helps prevent anyaccidental gas flow out of valve 22. It is noted to this effect thatalthough piston 218 has been shown with flat opposite top and bottomsurfaces, it can be made with convex opposite top and bottom surfacesthat have a same radius of curvature as that of the outer surface ofrotary valve member 214. Once the vacuum pump stops purging fluidsthrough vacuum channel 232, air at atmospheric pressure is injectedthrough air channel 234 to fill the void left by the previously purgedfluids. Thus, as the rotary valve member is rotated another 90°, allsolvent that might have been present between piston 218 and the housinginner wall, will have been previously purged, to prevent solvent frombeing accidentally exhausted to the atmosphere.

FIG. 6 shows another embodiment of a valve assembly 300 according to thepresent invention, which comprises a pair of valves 22 a, 22 b similarto valve 22 described hereinabove. A hopper 302 is installed atop valves22 a, 22 b, and a pair of tapered bottom openings 304, 306 in hopper 302provide access to the respective feedstock inlet openings 204, 204 ofthe valves 22 a, 22 b. A removable cover 308 allows access to the innerchamber of hopper 302. A pair of motors 310, 312 control the augers 208,208 of valves 22 a, 22 b. The respective feedstock outlet openings 206,206 of valves 22 a, 22 b open into a funnel 314 having a funnel outletopening 316 leading to the extraction chambers 24 (not shown in FIG. 6).

In use, valves 22 a, 22 b work in a similar manner than valve 22described hereinabove. Feedstock located in hopper 302 is gradually fedsimultaneously to both valves 22 a, 22 b through their respectivefeedstock inlet openings 204, 204. The feedstock is discharged at therespective outlet openings 306, 306 of valves 22 a, 22 b as describedhereinabove for valve 22, and funnel 314 directs the incoming feedstocktowards the entrance to the extraction chambers 24 (not shown in FIG.6).

In one embodiment, valves 22 a, 22 b will have regular cycles which areoffset relative to each other. More particularly, their respectiverotary valve members 214, 214 will be controlled so as to be angularlyoffset of 90° at all times, thus allowing an alternative feedstockdischarge from one valve 22 a, then the other 22 b.

In the embodiment of the invention illustrated in FIG. 1, there areshown five sequentially linked extraction chambers 24 a, 24 b, 24 c, 24d, 24 e. The feedstock is conveyed to extraction chambers 24 afterhaving been fed through inlet valve 22, is destined to be conveyed in acontinuous manner sequentially through all five of the extractionchambers 24, namely first through extraction chamber 24 a, then throughextraction chamber 24 b, and so on until it reaches extraction chamber24 e, after which it is conveyed outside of the extraction chamberassembly towards heating chamber 53.

Conveying means for conveying the solid product sequentially along theextraction chambers 24 are provided, for example in the form of a singleimpeller that extends throughout the entire extraction chamber assembly.

Within each extraction chamber 24, solvent is dispensed according todetermined extraction chamber solvent injection parameters. Moregenerally, extraction chambers 24 have determined extraction chamberparameters that will influence the oil extraction process therein. Theseextraction chamber parameters are set according to each oil-bearingsolid product being treated, according to the oil to be collected fromthe solid product, and according to the solvent being used. Theseparameters can further be modified from one extraction chamber 24 to theother if different extraction chamber parameters are desired indifferent extraction chambers 24. Parameters which can be modifiedinclude, but are not limited to: type of impeller used, including itsgeometry; rotation speed of impeller if it is a rotatable impeller suchas an auger; size of extraction chamber; flow rate of solvent beingdispensed in the extraction chamber 24; flow rate of miscella flowingout of the extraction chamber 24; manner of dispensing the solvent, suchas by providing particular solvent spray patterns; etc.

The purpose of controlling these parameters is to calibrate the oilleaching process within each extraction chamber 24, and consequently theentire oil leaching process throughout the extraction chamber assembly.Indeed, it will often be desirable to meet certain specific andrelatively precise oil recuperation parameters in the end product at theapparatus outlet, for example so as to maximize the oil recuperation orto reach determined oil proportions within the outputted solid product.

FIGS. 7 and 8 show one embodiment of an extraction chamber 24, whichdefines opposite upstream and downstream ends 400 and 402, respectively,and which comprises a hollow housing 404 defining an inner extractionchannel 406 extending between the extraction chamber upstream anddownstream ends 400, 402. The downstream end 402 of each extractionchamber 24 is in fluid communication with the upstream end 400 of thesequentially adjacent extraction chamber 24, until the last extractionchamber 24 e which communicates with heating chamber 53. Thus, sameextraction pressure and temperature values may be maintained throughoutextraction chambers 24. A power-driven impeller in the form of an auger408 extends through inner channel 406, with auger 408 extending throughthe entire extraction chamber assembly, from inlet valve 22 to outletvalve 26, including through heating chamber 53. Auger 408 also comprisesa number of agitation paddles 410 integrally attached thereto indesignated areas of extraction chamber 24. Spray nozzles 36, connectedto manifold 34, extend within inner channel 406.

In the embodiment shown in FIGS. 7 and 8, the particles of solid productare conveyed and agitated by auger 408 and are further agitated byagitation paddles 410 in a first portion of each extraction chamber 24so as to imbue a free-floating product particles flow patternconfiguration, for example according to the pattern shown in dottedlines at reference number 412 in FIG. 8. Simultaneously, spray nozzles36 will inject solvent in such a manner as to imbue the injected solventwith a vortex spray pattern configuration, for example according to thespray pattern schematically shown in dotted lines at reference number414 in FIG. 8. This solvent vortex pattern will carry some free-floatingsolid product particles in the vortex, which will enhance the effect ofthe solvent on the solid product particles, thus enhancing the leachingof oil.

Other alternate solvent injection means could also be envisioned bywhich solvent is injected in the extraction chambers to leach the oilfrom the solid products being circulated therein.

The solvent thus injected in extraction chamber 24 will leach a certainproportion of the oil from the oil-bearing product, to form a miscelladefined as a mixture of solvent and oil.

Downstream of spray nozzles 36 in extraction chamber 24, is provided amiscella collection trough 416 underneath a filter 418. The miscella,carried by impeller 408, will flow and be collected in trough 416, withthe solid product particles being retained by filter 418 within channel406. It is understood that a suitable filter will be selected accordingto the type of solvent being used, the type of oil being collected, andthe type of solid product being processed. The miscella collected intrough 416 will be carried away through a corresponding miscella outletchannel 38 (FIG. 1) communicating with trough 416.

Extraction chamber 24 consequently defines two different operativeportions, namely a first solvent injection portion where solvent isinjected in the agitated solid material particles, and a second miscellacollecting portion where miscella is collected. Agitation paddles 410and spray nozzles 36 are present only in the solvent injection portion,and filter 418 and trough 416 are present only in the miscellacollecting portion.

According to the invention, it can thus be seen that there is provided acontinuous process for extracting oil from an oil-bearing solid product,by which the solid product is continuously fed through inlet valve 22,continuously circulated through extraction chambers 24, and continuouslycollected at outlet vale 26. Simultaneously, in each extraction chamber24, a certain proportion of oil is continuously extracted from theoil-bearing product, whereby a final proportion of oil is extracted atthe outlet of the entire extraction chamber assembly. It is envisioned,according to one embodiment, to provide suitable sensors of knownconstruction (not shown), similar to sensor 51, to detect the proportionof oil remaining in the solid product at the outlet of each extractionchamber 24, and to use a control mechanism (not shown) to dynamicallycontrol the extraction chamber parameters in each extraction chamber 24so as to obtain a desired remaining oil proportion in the solid productsat the outlet of apparatus 20. For example, if it is predetermined that50%, 90% or even 100% of the oil is to be recuperated from the solidproduct, then the control mechanism could dynamically control distinctlyin each extraction chamber 24 the solvent flow rate, the solvent spraypattern configuration, the rotation speed of the impelling auger, andany other extraction chamber parameter, to modify the oil extractionparameters to obtain the desired result according to the oil proportiondetected at the outlet of each extraction chamber 24.

According to the present invention, the series of extraction chambers 24through which the solid product is sequentially conveyed will allow forup to a very important proportion (if desired), if not all, of the oilto be extracted from the solid product. Indeed, each pass of the solidproduct through one extraction chamber 24 allows oil to be leached outof the solid product, and consequently providing a series of extractionchambers 24 allows the proportion of oil in the solid product toinversely exponentially tend towards zero, and even eventually reachzero. This oil extraction may also be calibrated by means of the dynamiccontrol over oil extraction within the extraction chambers as describedabove. Indeed, contrarily to the prior art known to applicant, thepresent invention makes use of a process for extracting oil in which theextraction chamber parameters may be modified during the operation ofapparatus 20 according to the results that are detected by the sensors,either at the apparatus outlet, and/or at the outlet of every individualextraction chamber 24. By dynamically controlling and eventuallymodifying the extraction chamber parameters such as the solvent spraypatterns and flow rate and the impeller speed, for example, theproportion of oil extraction may thus be selectively controlled.

In addition to relying on the sequence of extraction chambers, theselective proportion of oil extraction also relies on the manner bywhich the oil is extracted within each extraction chamber. Indeed, notonly can the extraction chamber parameters be dynamically modified, butthe particular agitation of the solid product particles within eachextraction chamber 24, together with the vortexes of solvent beingcreated by spray nozzles 36 in each extraction chamber 24, provide forthe possibility of a high extraction rate in each extraction chamber 24.

It is understood that a high extraction rate is only referred to hereinas a choice or possibility for the operator of apparatus 20. Indeed,while in some cases maximum oil extraction may be desirable such as inthe case of soil decontamination, in other cases such as in thepreparation of foodstuff a certain proportion of oil content in theoutputted solid product may be desirable.

Having an extraction pressure above ambient pressure, for example atapproximately 10 bars, is advantageous not only because it allows theuse of a solvent in liquid state which would normally be in gazeousstate at ambient pressure, for a given temperature value, but alsobecause it increases the efficiency of the process. Indeed, filters 418with a finer mesh may be used through which the miscella will betransferred, if the extraction pressure is important, to promote thepassage of miscella through the filters 418.

It is noted that the respective separation pressure and extractionpressure within separation unit 48 and extraction chambers 24respectively, may differ.

An alternate embodiment of the invention is shown in FIG. 9, where abatch process apparatus 500 is schematically shown. Apparatus 500comprises an extraction chamber 502 including a feedstock inlet 504,which can be closed by a door (not shown) once feedstock is fed intoextraction chamber 502. Extraction chamber 502 includes a first coarsefilter 506, and an outlet 508 leading to a second fine filter 510. Inuse, a batch of feedstock comprising solid oil-bearing product is fedthrough feedstock inlet 504, the door to the extraction chamber 502 isthen closed, and the batch oil extraction process can then begin.

For the oil extraction to be accomplished, solvent from a main solventtank 512 is injected into extraction chamber 502 by means of a solventinjection pump 514. Solvent thus injected leaches a certain proportionof the oil from the oil-bearing product to form a miscella comprising amixture of oil and solvent. The miscella is collected through the coarsefilter 506 while the coarse solid product particles are retained inextraction chamber 502, and then through fine filter 510 while fineparticulate solid product is retained by fine filter 510. The miscellathus collected is conveyed to a liquid-liquid separation unit 516 wherethe oil is separated from the solvent through a suitable liquid-liquidseparation process such as one of molecular weight, specific gravity andviscosity differential separation processes. Solvent separated from theoil is conveyed back to main solvent tank 512, while oil separated fromthe solvent is collected at an oil outlet 518.

There is also provided a solvent vapor circuit 520 including a solventvapor pump 522 that will convey residual solvent vapor from extractionchamber 502 to carry the solvent back into solvent tank 512 where itwill precipitate into liquid state, once a batch of solid material hasbeen treated. This prevents solvent vapor from being exhausted to theatmosphere once the door to the extraction chamber 502 is opened toremove the solid product from therein.

In the embodiment of FIG. 9, the pressure and temperature values arealso controlled in extraction chamber 502 and in main solvent tank 512to maintain the solvent mainly in liquid state throughout theclosed-loop circuit of the solvent. Any solvent vapor conveyed by pump522 back into tank 512 is subjected to temperature and pressureconditions that will make the solvent vapor precipitate. As with thefirst embodiment showing a continuous process, the solvent remainingmainly in liquid-state throughout its closed-loop circuit prevents anyheat from having to be used to separate the oil from the solvent byevaporating the solvent. This absence of heat helps prevent denaturingof the oil.

Any further modification to the present invention, which does notdeviate from the scope of the appended claims as will be obvious for aperson skilled in the art, is further considered to be included herein.

1-20. (canceled)
 21. A process for separating a solute from asolute-bearing product, comprising: conveying the solute-bearing productthrough an extraction chamber in a free-floating flow patternconfiguration; spraying a solvent into the extraction chamber to contactthe solute-bearing product in the free-floating flow patternconfiguration and extract the solute from the solute-bearing product;collecting a mixture of the extracted solute and solvent from theextraction chamber; and separating the extracted solute from thesolvent.
 22. The process of claim 21, wherein the solute is soluble inthe solvent at extraction pressure and temperature.
 23. The process ofclaim 21, wherein the solvent is in a gaseous state at ambienttemperature and pressure values, but is maintained in a liquid state inthe extraction chamber at extraction pressure and temperature values.24. The process of claim 21, wherein the solvent is comprised of atleast one composition selected from the group consisting of propane,butane and refrigerant.
 25. The process of claim 21, wherein thesolute-bearing product is a solid containing oil, fat or a mixturethereof.
 26. The process of claim 25, wherein the solid product iscomprised of rendered animal tissue; industrial, commercial or domesticoleiferous wastes; oleiferous hazards; oleiferous industrial byproducts;oil bearing sands; strata; mineral; rock formation; fried or soakedsubstances inedible and edible; legumes; legumes and their hulls andcasings; seeds; seeds and their hulls, casings or shells; nuts; nuts andtheir hulls, casings or shells; tree leaves; tree branches; tree roots;plant leaves; plant stems; basal leaves and branches and roots, marinelife; field crops; and vegetables.
 27. A process for extracting solutefrom a solute-bearing product, comprising: feeding particles of thesolute-bearing product to an extraction chamber; agitating the particlesof solute-bearing product to promote the formation of free-floatingparticles flowing through the extraction chamber; and injecting solventinto the extraction chamber to contact the free-floating particles andextract the solute from the solute-bearing product.
 28. The process ofclaim 27, wherein the solute is soluble in the solvent at extractionpressure and temperature.
 29. The process of claim 27, wherein thesolvent is in a gaseous state at ambient temperature and pressurevalues, but is maintained in a liquid in the extraction chamber state atextraction pressure and temperature values.
 30. The process of claim 27,wherein the solvent is comprised of at least one composition selectedfrom the group consisting of propane, butane and refrigerant.
 31. Theprocess of claim 27, wherein the solute-bearing product is a solidcontaining oil, fat or a mixture thereof.
 32. The process of claim 31,wherein the solid product is comprised of rendered animal tissue;industrial, commercial or domestic oleiferous wastes; oleiferoushazards; oleiferous industrial byproducts; oil bearing sands; strata;mineral; rock formation; fried or soaked substances inedible and edible;legumes; legumes and their hulls and casings; seeds; seeds and theirhulls, casings or shells; nuts; nuts and their hulls, casings or shells;tree leaves; tree branches; tree roots; plant leaves; plant stems; basalleaves and branches and roots, marine life; field crops; and vegetables.33. The process of claim 27, further comprising collecting a mixture ofthe extracted solute and solvent from the extraction chamber.
 34. Theprocess of claim 27, further comprising separating the extracted solutefrom the solvent.
 35. A process for extracting solute from asolute-bearing product, comprising: feeding particles of thesolute-bearing product to an extraction chamber; conveying the particlesof solute-bearing product through the extraction chamber in the form ofa free-floating flow pattern configuration; and spraying a solvent intothe extraction chamber to contact the solute-bearing product in thefree-floating flow pattern configuration and extract the solute from thesolute-bearing product.
 36. The process of claim 35, wherein the soluteis soluble in the solvent at extraction pressure and temperature. 37.The process of claim 35, wherein the solvent is in a gaseous state atambient temperature and pressure values, but is maintained in a liquidstate in the extraction chamber at extraction pressure and temperaturevalues.
 38. The process of claim 35, wherein the solvent is comprised ofat least one composition selected from the group consisting of propane,butane and refrigerant.
 39. The process of claim 35, wherein thesolute-bearing product is a solid containing oil, fat or a mixturethereof.
 40. The process of claim 39, wherein the solid product iscomprised of rendered animal tissue; industrial, commercial or domesticoleiferous wastes; oleiferous hazards; oleiferous industrial byproducts;oil bearing sands; strata; mineral; rock formation; fried or soakedsubstances inedible and edible; legumes; legumes and their hulls andcasings; seeds; seeds and their hulls, casings or shells; nuts; nuts andtheir hulls, casings or shells; tree leaves; tree branches; tree roots;plant leaves; plant stems; basal leaves and branches and roots, marinelife; field crops; and vegetables.
 41. The process of claim 35, furthercomprising collecting a mixture of the extracted solute and solvent fromthe extraction chamber.
 42. The process of claim 35, further comprisingseparating the extracted solute from the solvent.
 43. A process forseparating a solute from a solute-bearing solid product, comprising:feeding the solute-bearing product into an extraction chamber; injectingsolvent into the extraction chamber to contact the solute-bearingproduct and extract the solute from the solute-bearing product;injecting a vapor unreactive with the solvent into the extractionchamber to maintain extraction pressure in the extraction chamber abovean ambient pressure value during extraction of the solute from thesolute-bearing product; collecting a mixture of the extracted solute andsolvent from the extraction chamber; and separating the extracted solutefrom the solvent.
 44. The process of claim 43, wherein the vapor issolvent vapor.
 45. The process of claim 43, wherein the solvent issolute with in the solvent at extraction pressure and temperature. 46.The process of claim 43, wherein the solvent is in a gaseous state atambient temperature and pressure values, but is maintained in a liquidstate in the extraction chamber at extraction pressure and temperaturevalues.
 47. The process of claim 43, wherein the solvent is comprised ofat least one composition selected from the group consisting of propane,butane and refrigerant.
 48. The process of claim 43, wherein thesolute-bearing product is a solid containing oil, fat or a mixturethereof.
 49. The process of claim 48, wherein the solid product iscomprised of rendered animal tissue; industrial, commercial or domesticoleiferous wastes; oleiferous hazards; oleiferous industrial byproducts;oil bearing sands; strata; mineral; rock formation; fried or soakedsubstances inedible and edible; legumes; legumes and their hulls andcasings; seeds; seeds and their hulls, casings or shells; nuts; nuts andtheir hulls, casings or shells; tree leaves; tree branches; tree roots;plant leaves; plant stems; basal leaves and branches and roots, marinelife; field crops; and vegetables.
 50. A process for separating a solutefrom a solute-bearing solid product, comprising: feeding thesolute-bearing product into an intermediate chamber; removing air fromthe intermediate chamber; conveying the solute-bearing product from theintermediate chamber to an extraction chamber; injecting solvent intothe extraction chamber to contact the solute-bearing product and extractthe solute from the solute-bearing product; injecting a vapor into theextraction chamber to maintain extraction pressure in the extractionchamber above an ambient pressure value during extraction of the solutefrom the solute-bearing product; and recovering the extracted solute.51. The process of claim 50, wherein the vapor is solvent vapor.
 52. Theprocess of claim 50, wherein the solute is soluble in the solvent atextraction pressure and temperature.
 53. The process of claim 50,wherein the solvent is in a gaseous state at ambient temperature andpressure values, but is maintained in a liquid state in the extractionchamber at extraction pressure and temperature values.
 54. The processof claim 50, wherein the solvent is comprised of at least onecomposition selected from the group consisting of propane, butane andrefrigerant.
 55. The process of claim 50, wherein the solute-bearingproduct is a solid containing oil, fat or a mixture thereof.
 56. Theprocess of claim 55, wherein the solid product is comprised of renderedanimal tissue; industrial, commercial or domestic oleiferous wastes;oleiferous hazards; oleiferous industrial byproducts; oil bearing sands;strata; mineral; rock formation; fried or soaked substances inedible andedible; legumes; legumes and their hulls and casings; seeds; seeds andtheir hulls, casings or shells; nuts; nuts and their hulls, casings orshells; tree leaves; tree branches; tree roots; plant leaves; plantstems; basal leaves and branches and roots, marine life; field crops;and vegetables.
 57. The process of claim 50, further comprisingseparating the extracted solute from the solvent.